Problem at Low Loads with Inverted-Loop Superheaters
Problem at Low Loads with Inverted-Loop Superheaters
In tall inverted-loop superheater of the type shown earlier, one of the concerns is that the steam-side pressure drop should be larger than the gravity head to ensure flow in the downward direction; this situation arises at low loads in circuits with downward flow when the friction loss is low and is on par with gravity loss.
Figure 3.37 shows the variation of friction and gravity loss as a function of mass flow of steam in downward and upward flow section of a superheater. When steam flows upward, both the gravity loss and friction loss are additive, and hence, the sum is always positive as shown and the curve is monotonic. In the downward flow section, at low flows, the enthalpy pickup in a semi-radiant superheater will be more than in a convective superheater, and the specific volume increases resulting in lower density of steam and lower gravity loss. As the steam flow increases, the temperature and specific volume of steam reach a steady value, and the density of steam will also reach a high value and be leveled out, while the friction loss increases as the square of the flow. The gravity loss versus mass flow curve will have
a shape as shown with two likely operating points at low loads. It shows that at higher mass flows, we do not have a problem (as far as stagnation is concerned, but overheating due to low steam velocity or direct furnace radiation is another issue) as we get into the region where the friction loss overtakes the gravity loss and be in the positive slope region. However, at low loads, it is showing an ambiguous trend where for a given pressure drop, there are two possible flows, which is an unstable characteristic; any small nonuniformity in gas-side or steam-side flows can upset the flows in a given tube and place the tube in a vulnerable spot resulting in overheating due to stagnation or even reverse flow.
This trend may be exhibited even with a convective superheater with low steam-side pressure drop located behind a large screen section, but due to the lower gas temperature at low loads, the superheater is in a much safer region. When consultants specify a low steam-side pressure drop, they should also be concerned about the superheater design and the lowest load it can operate without possible stagnation concerns.
It may be noted that the curve of the furnace exit gas temperature versus heat input has
a small slope, and hence, even at low loads, the energy absorbed by the superheater in the
Δp
Δp Friction loss Total loss
h Total loss h
Δp m 1 m 2 Mass flow
Gravity loss
Δp
Friction loss
Gravity loss
0 Mass flow
Ambiguous region –Δp
Upward flow Downward flow
FIGURE 3.37
Variation of pressure drop with flow in downward flow section of superheater.
138 Steam Generators and Waste Heat Boilers: For Process and Plant Engineers
semi-radiant zone is significant (that is why the author insists on a large screen section ahead of the superheater and always design a convective-type superheater). Hence, the design should have ensured that at the minimum load, the steam pressure drop is high enough to overcome gravity loss; else, a horizontal tube design or some other configura- tion should have been selected for the superheater by the boiler designer.
To overcome the problem at low loads, a baffle was suggested in the inlet header as shown in Figure 3.36. The introduction of the baffle as shown increased the tube-side velocity and friction loss about eight times more; due to the higher tube-side heat transfer coefficient, the tubes were also cooler at full load. As the flow direction is now parallel-flow, the first- pass exit will see a lower steam temperature as well as low tube wall temperature, and the second-pass exit is located in a much cooler gas temperature region minimizing the exter- nal radiation concerns. The final desired steam temperature is reached in a much cooler gas temperature zone, and hence, the tubes will be running cooler than in the option without a baffle in the header. A large turndown is also now possible due to the higher pressure drop.
Parts
» For Process and Plant Engineers
» A Few Typical Solved Problems
» Excess Air from Flue Gas Analysis
» Simplified Combustion Calculations
» Relating Oxygen and Energy Input in Turbine Exhaust Gases
» Evaluating Fuel Quantity Required to Raise Turbine Exhaust Gas Temperature
» Simplified Formulae for Boiler Efficiency
» Firing Fuels with Low Heating Values
» Boiler duty and efficiency calculations
» Acid Dew Point Temperature T dp
» Steam Generator Furnace Design
» Advantages of Water-Cooled Furnaces
» Furnace Exit Gas Temperature Evaluation
» Empirical Formula for Furnace Duty Estimation
» Distribution of Radiation to Tube Banks
» External Radiation to Heat Transfer Surfaces at Furnace Exit
» Correlations for CHF (Critical Heat Flux) and Allowable Steam Quality
» Guidelines for Good Circulation System Design
» Emissions Affect Steam Generator Designs
» Adding Condensate Heater to Improve Boiler Plant Efficiency
» Understanding Boiler Surface Areas
» Steam Generators for Oil Sands Application
» Radiant versus Convective Superheaters
» Steam Inlet and Exit Nozzle Location
» Case Study of a Superheater with Tube Failure Problems
» Problem at Low Loads with Inverted-Loop Superheaters
» Data Required for Performing Steam Generator Analysis
» Evaluating Part Load Performance
» Tube Wall Temperature Estimation at Economizer Inlet
» Methods to Minimize Low-Temperature Corrosion Problems
» Water Chemistry, Carryover, Steam Purity
» Sizing and Performance Calculations
» Flue Gas Composition and Gas Pressure
» Heat Recovery in Sulfur Plants
» Heat Recovery in Sulfuric Acid Plant
» Heat Recovery in Hydrogen Plants
» Combining Solar Energy with Heat Recovery Systems
» Natural versus Forced Circulation HRSGs
» Optimizing Pinch and Approach Points in HRSGs
» HRSG Performance and Evaluating Field Data
» Advantages of Supplementary Firing in HRSGs
» Performance with and without Export Steam
» Cement Plant Waste Heat Recovery
» Fluid Heaters and Film Temperature
» Boiling Heat Transfer Coefficient h o
» Off-Design Performance with Addition of Economizer
» Simulation of Fire Tube Boiler Performance
» Simplified Approach to Evaluating Performance of Fire Tube Boilers
» Heat Transfer Inside and Outside Tubes
» Specifying Waste Heat Boilers
» Understanding Pinch and Approach Points
» Estimating Steam Generation and Gas–Steam Temperature Profiles
» Why Cannot We Arbitrarily Select the Pinch and Approach Points?
» Off-Design Performance Evaluation
» Single- or Multiple-Pressure HRSG
» Cogeneration Plant Application
» Water Dew Point of Flue Gases
» Condensation Heat Transfer Calculations
» Condensation over Finned Tubes
» Drum Coil Heater: Bath Heater Sizing
» Checking Heat Transfer Equipment for Noise and Vibration Problems
» Steam Drum Calculations Steam Velocity in Drum
» Flow Instability in Two-Phase Circuits
» Superheater Design and Off-Design Calculation
» NTU Method of Performance Evaluation (Number of Transfer Units)
» Appendix B: Tube-Side Heat Transfer Coefficients and Pressure Drop
» Another Method of Estimating h c for Water
» Importance of Streams in Superheater, Economizer
» Simplified Procedure for Evaluating Performance of Plain Tube Bundles
» Appendix D: Nonluminous Heat Transfer Calculations
» Determination of Heat Transfer Coefficient h c Convective Heat Transfer Coefficient
» How Is Life of Superheater Affected by High Tube Wall Temperatures?
» Effect of h i on Fin Selection
» Reduce Weight of Tube Bundles Using Smaller Tubes
» Effect of Outside Fouling Factor
» Effect of Fin Thickness and Conductivity
» Why Are Fins Not Used in Gas–Gas Exchangers?
» Appendix F: Properties of Gases
» Flue Gas Mixture Properties Calculation
» Appendix G: Quiz on Boilers and HRSGs with Answers
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